EP2310322B1 - Procédés de fabrication de dioxyde de titane - Google Patents

Procédés de fabrication de dioxyde de titane Download PDF

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EP2310322B1
EP2310322B1 EP08797260.0A EP08797260A EP2310322B1 EP 2310322 B1 EP2310322 B1 EP 2310322B1 EP 08797260 A EP08797260 A EP 08797260A EP 2310322 B1 EP2310322 B1 EP 2310322B1
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Prior art keywords
iron
rich
oxalate
precipitate
solution
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EP2310322A1 (fr
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David Richard Corbin
Scott N. Hutchison
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Chemours Co TT LLC
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Chemours Co TT LLC
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G23/00—Compounds of titanium
    • C01G23/04—Oxides; Hydroxides
    • C01G23/047—Titanium dioxide
    • C01G23/053—Producing by wet processes, e.g. hydrolysing titanium salts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G23/00—Compounds of titanium
    • C01G23/04—Oxides; Hydroxides
    • C01G23/047—Titanium dioxide
    • C01G23/08—Drying; Calcining ; After treatment of titanium oxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G49/00—Compounds of iron
    • C01G49/02—Oxides; Hydroxides
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK  ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
    • C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
    • C09C1/36—Compounds of titanium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/16—Extraction of metal compounds from ores or concentrates by wet processes by leaching in organic solutions
    • C22B3/1608—Leaching with acyclic or carbocyclic agents
    • C22B3/1616—Leaching with acyclic or carbocyclic agents of a single type
    • C22B3/165—Leaching with acyclic or carbocyclic agents of a single type with organic acids
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1236—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching
    • C22B34/124—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching using acidic solutions or liquors
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/10—Obtaining titanium, zirconium or hafnium
    • C22B34/12—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08
    • C22B34/1236—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching
    • C22B34/1259—Obtaining titanium or titanium compounds from ores or scrap by metallurgical processing; preparation of titanium compounds from other titanium compounds see C01G23/00 - C01G23/08 obtaining titanium or titanium compounds from ores or scrap by wet processes, e.g. by leaching treatment or purification of titanium containing solutions or liquors or slurries
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates to processes for the production of titanium dioxide from ilmenite.
  • Titanium dioxide is used as a white pigment in paints, plastics, paper, and specialty applications.
  • Ilmenite is a naturally occurring mineral containing both titanium and iron with the chemical formula FeTiO 3 .
  • WO2008/082384 discloses a process for the production of titanium dioxide from ilmenite, said process comprising digesting ilmenite with aqueous ammonium hydrogen oxalate.
  • the present invention provides new processes for TiO 2 production with the ability to use low grade ores that are less energy intensive, that require reduced capital investment and that have a smaller environmental footprint than conventional current production processes.
  • FIGURE 1 is a process flow diagram of a process according to one embodiment of the present invention for making titanium dioxide.
  • One aspect of the present invention is a process comprising:
  • ilmenite is digested by exposure to aqueous trimethylammonium hydrogen oxalate.
  • Trimethylammonium is defined as three methyl groups and one hydrogen bound to a nitrogen atom.
  • the processes include digesting ilmenite with trimethylammonium hydrogen oxalate. This forms an iron-rich precipitate and a titanium-rich solution, which can be separated. A variety of further processing steps can lead to the production of titanium dioxide.
  • oxalate in process streams can be recycled into trimethylammonium hydrogen oxalate for further digestion.
  • a schematic of one embodiment of the present invention is shown as Figure 1 .
  • Ore is digested in the first step of the process. Digestion yields an iron-rich solid and a titanium-rich solution. The titanium-rich solution is hydrolyzed and the resulting solution is crystallized into titanium dioxide. The iron-rich solid can be hydrolyzed to form an iron oxide.
  • Aqueous ditrimethylammonium oxalate can be collected from several process steps. The aqueous di-trimethylammonium oxalate can be heated to give aqueous trimethylammonium hydrogen oxalate and aqueous trimethylamine which can be recycled to earlier process steps.
  • the term "ilmenite ore” refers to iron titanate with a titanium dioxide content ranging from 35 to 75% by weight.
  • the chemical composition of natural ilmenite ore can vary. It is commonly understood to be ferrous titanate with the formula FeTiO 3 .
  • the iron proportions can be higher than the theoretical composition due to admixed hematite or magnetite. An excess of titanium may be present, due to the presence of rutile.
  • the processes of the present invention can be used for ilmenites with titanium dioxide content on the lower end of the ilmenite range. A titanium dioxide content of 35 to 60% by weight is preferred and a content of 45 to 55% by weight is most preferred.
  • the particle size of the ilmenite is preferably in the range of less than 1 to 300 ⁇ m for rapid dissolution, with 95% or more of the particles below ⁇ 100 ⁇ m. Smaller sized ore particles ( ⁇ 140 mesh ( ⁇ 105 ⁇ m)) can be used in this process and may provide an advantage over the known sulfate and chloride processes. These smaller particles are not preferred for use in prior sulfate or chloride processes.
  • concentration of the trimethylammonium hydrogen oxalate is necessarily 5 to 10 molal.
  • the digestion reaction may be conducted in one of three different chemical environments - non-oxidative, oxidative, or reductive. All digestion reaction environments contain aqueous trimethylammonium hydrogen oxalate. The ratio of trimethylammonium to hydrogen in the aqueous trimethylammonium hydrogen oxalate may vary. The digestions may be conducted in aqueous trimethylammonium hydrogen oxalate where the trimethylammonium to hydrogen ratio is up to and including 1.5 to 1.
  • the ilmenite is contacted with aqueous trimethylammonium hydrogen oxalate while under an atmosphere of an inert gas such as nitrogen.
  • an inert gas such as nitrogen.
  • suitable inert gasses include helium and argon. Digestion under inert gas inhibits the oxidation of iron ions in solution.
  • the molar ratio of trimethylammonium hydrogen oxalate to ilmenite ore is 4:1 to 8:1 (on the basis of hydrogen in the trimethylammonium hydrogen oxalate to ilmenite ratio) for digestion performed in an inert atmosphere.
  • a mixture is formed of the ilmenite and aqueous trimethylammonium hydrogen oxalate.
  • This mixture is held under reflux conditions at a temperature of about 100 °C to 140 °C until most of the ore, e.g., at least about 70%, preferably at least about 90%, in some embodiments substantially all, of the ore is dissolved.
  • dissolution of the ilmenite in the aqueous trimethylammonium hydrogen oxalate occurs at a rate such that generally about 70 to 90 percent of the titanium in the ore is dissolved within about 8 hours. While dissolution can be carried out for longer than 8 hours, it may not be desirable to do so, or advantageous in terms of cost.
  • the iron(II) in solution precipitates as FeC 2 O 4 ⁇ 2H 2 O leaving a titanium-rich solution.
  • a titanium-rich solution is one in which the molar ratio of Ti/(Fe+Ti) in the solution is greater than that present in the ilmenite ore used; , e.g., a ratio of 50.1:100 or greater for an ideal FeTiO 3 . It is preferred that the amount of iron in the leachate is minimized.
  • An iron-rich precipitate is one in which the molar ratio of Ti/(Fe+Ti) in the solution is less than that present in the ilmenite ore used. The precipitate contains FeC 2 O 4 ⁇ 2H 2 O.
  • the solids from this digestion step can also contain unreacted ilmenite ore and its accompanying impurities (e.g., quartz, zircon, rutile, anatase, other iron titanates, monazite, etc).
  • impurities e.g., quartz, zircon, rutile, anatase, other iron titanates, monazite, etc.
  • other very insoluble metal oxalates can be present (e.g., magnesium oxalate, calcium oxalate, etc.).
  • Non-oxidative digestion can be carried out in the presence of a reducing agent in addition to the trimethylammonium hydrogen oxalate.
  • the reducing agent can be, for example, Fe(0), Zn(0), Ti(III), or Al(0). Iron metal is preferred.
  • Treating with a reducing agent desirably converts substantially all of the Fe(III) present, which is highly soluble in the aqueous trimethylammonium hydrogen oxalate, to Fe(II), which precipitates as FeC 2 O 4 ⁇ 2H 2 O, further increasing the Ti/(Ti+Fe) ratio of the solution.
  • the solution can then be diluted to about 1 wt % Ti as determined by ICP (inductively coupled plasma spectrometry) or equivalent chemical analysis technique.
  • the metal reducing agent can be added as powder, chips, wire or other known forms.
  • Other metal oxalates from impurities in the ilmenite ore such as MnC 2 O 4 ⁇ 2H 2 O can coprecipitate with the iron oxalate.
  • oxidative digestion the digestion is carried out in an oxidative atmosphere such as air.
  • the trimethylammonium hydrogen oxalate to ore molar ratio is 5:1 to 10:1 (on the basis of hydrogen in the trimethylammonium hydrogen oxalate to ilmenite ratio) for dissolution performed in air or other oxidative atmosphere.
  • Fe(II) species are oxidized to Fe(III).
  • the ferric ions produced upon digestion in air are more soluble in the solution than the ferrous ions and require additional steps to reduce and separate in order to form a titanium-rich solution for further processing.
  • Oxidative digestion involves contacting ilmenite ore with aqueous trimethylammonium hydrogen oxalate in an oxidative atmosphere to form a solution rich in iron and titanium and a solid containing non-dissolvable material.
  • Air can be added as overpressure in an autoclave, for example, using a sparger.
  • Insoluble components of the ore can include rutile, zircon, and/or quartz.
  • a reducing agent such as zinc metal under inert atmosphere to reduce the ferric ions to ferrous ions and to form an iron-rich precipitate.
  • the digestion is carried out in the presence of reducing agents such as iron, zinc, magnesium or aluminum metal particles added at the start of the digestion.
  • reducing agents such as iron, zinc, magnesium or aluminum metal particles added at the start of the digestion.
  • substantially all ferrous ions are formed, leading to formation of an iron-rich precipitate which can be separated from the titanium-rich solution.
  • the product of the digestion is a titanium-rich solution and an iron-rich precipitate.
  • the titanium-rich solution is separated from the iron-rich precipitate by conventional methods such as filtration and centrifugation.
  • Sufficient trimethylammonium hydrogen oxalate can be added to give a saturated solution at hydrolysis temperatures (between 25 °C and 90 °C; preferably 75-90 °C).
  • the titanium-rich solution is hydrolyzed with trimethylamine or aqueous trimethylamine, preferably aqueous trimethylamine.
  • the trimethylamine in the form of gas or aqueous solution, may be added to the titanium-rich solution at a temperature of about 25 °C to about 90 °C, preferably 75 °C to 90 °C, in sufficient quantities to maximize the precipitation of the titanium component and minimize the precipitation of the iron component of the titanium-rich solution.
  • This is generally monitored by pH. For example, if the hydrolysis is performed at room temperature (about 25 °C), the pH is preferably no higher than about 7.5. Higher pH can lead to the undesired precipitation of iron species, which can require extensive washing and bleaching with acid to remove.
  • the product of the hydrolysis is a mixture containing a high oxalate content "titanyl hydroxide” solid and an oxalate-rich residual solution.
  • the chemical identity of "titanyl hydroxide” is not precisely known, in part because the degree of hydration is variable.
  • the "titanyl hydroxide” (titanic acid) is believed to exist as TiO(OH) 2 , TiO(OH) 2 ⁇ H 2 O or TiO(OH) 2 ⁇ nH 2 O (where n > 1) or mixtures thereof [see J. Barksdale, "Titanium: Its Occurrence, Chemistry and Technology", 2nd Edition, Ronald Press; New York (1966 )].
  • the mixture may be allowed to stir for 1 or more hours and is then separated, preferably by hot filtering through a filter medium with pore size of approximately 4 ⁇ m - 5.5 ⁇ m. Filtration rates of greater than about 12 mL/min are preferred.
  • the titanyl hydroxide solids are then washed with a material selected from the group consisting of water, trimethylamine and aqueous trimethylamine to form low oxalate titanyl hydroxide.
  • Titanium dioxide is known to exist in at least three crystalline mineral forms: anatase, rutile and brookite.
  • Crystallization of titanium dioxide from the low oxalate-containing titanyl hydroxide solids can be accomplished by one of four crystallization processes: low temperature hydrothermal (150 °C - 250 °C), high temperature hydrothermal (250 °C - 374 °C), normal calcination (700 °C - 1100 °C) or flux calcination. Crystallization can optionally involve addition of crystallization aids such as, for example, rutile seed, mineralizers, and rutile directors (e.g., Sn compounds). The higher temperature routes - both hydrothermal and calcination - can give rutile of the proper particle size to give the product the desired opacity for most applications. Titanium dioxide product in the particle size range 100 to 600 nanometers is desired for use as pigment. Titanium dioxide with a particle size less than 100 nanometers is referred to as nano-sized.
  • the low oxalate containing titanyl hydroxide solids are heated at a temperature of about 800 °C to 1000 °C for a period of at least one hour.
  • the solids can be heated in air or in an inert atmosphere.
  • Conversion of low oxalate containing titanyl hydroxide solids into crystalline anatase form and rutile form can be influenced by process factors including, for example, temperature, time at temperature, temperature-time profile, amount of impurities, and additives that promote formation or stabilization of anatase, rutile or brookite.
  • process factors including, for example, temperature, time at temperature, temperature-time profile, amount of impurities, and additives that promote formation or stabilization of anatase, rutile or brookite.
  • the same or other factors also affect the primary and secondary titania particle morphologies, e.g., size, shape, aggregation, and agglomeration, of the titania product.
  • the morphology of rutile made from low oxalate containing titanyl hydroxide solids can be changed by use of an additive such as a fluxing agent.
  • a fluxing agent such as sodium chloride is an example of a fluxing agent.
  • Addition of NaCl can modify the shape and size of the primary and secondary rutile particles. This is referred to as "flux calcination".
  • flux calcination the titanium precipitate is heated to about 800 °C to 1000 °C for a period of at least 1 h in the presence of at least 1 wt % of a fluxing agent such as NaCl.
  • fluxing agent such as NaCl.
  • examples of other fluxing agents are KCI and LiCl. Addition of NaCl during calcination can provide a product containing larger primary particles having a more clearly defined shape.
  • NaCl can also serve as a structure-directing agent (rutile promoter).
  • rutile promoter For example, in the absence of NaCl, leachate-derived titanium precipitate produces irregularly-shaped particles of anatase, both with and without additional particle-morphology modifiers (such as K and P), at 800 °C. However, modifying the process conditions by addition of as little as about 1-5 wt % NaCl (the percent based on the weight of TiO 2 that can be obtained from the precipitate) produces a well-defined rutile particle product at 800 °C.
  • Sodium chloride therefore, can be used with oxalate-derived titanium precipitate as a rutile promoter, a particle morphology control agent, and particle agglomeration control agent at 800 °C.
  • Other agents such as KCI and LiCl can also be used with oxalate-derived titanium precipitate as a rutile promoter, a particle morphology control agent, and particle agglomeration control agent at 800 °C
  • Low temperature hydrothermal crystallization involves conversion of the amorphous "titanyl hydroxide" intermediate to TiO 2 in the presence of water at relatively mild temperature conditions (from 150 °C to 250 °C) compared to the calcination temperatures (ca. 1000+ °C) typically utilized in current commercial TiO 2 production.
  • Reaction temperatures in the LTHC process range from as low as 150 °C up to 250 °C with reaction pressures on the order of the corresponding vapor pressure of water and with reaction times of less than 24 hours. Variation within this range of conditions, control of the acid concentration in the reaction mixture, and the addition of phase-directing mineralizers can be utilized to selectively control the resulting TiO 2 particle size, crystallography, and morphology.
  • rutile TiO 2 of pigmentary size can be formed at 220 °C - 250 °C with the addition of a rutile-directing mineralizer (e.g., ZnCl 2 , ZnO, MgCl 2 , or NaCl).
  • a rutile-directing mineralizer e.g., ZnCl 2 , ZnO, MgCl 2 , or NaCl.
  • Nano-sized rutile TiO 2 can be produced under similar conditions, but at temperatures as low as 150 °C. Operation at temperatures as low as 150 °C with anatase-directing mineralizers (e.g., KH 2 PO 4 , Al 2 (SO 4 ) 3 , ZnSO 4 , and Na 2 SO 4 ) produces anatase TiO 2 .
  • anatase-directing mineralizers e.g., KH 2 PO 4 , Al 2 (SO 4 ) 3 , ZnSO 4 , and Na 2 SO 4
  • Brookite TiO 2 can be prepared at temperatures above 150 °C, optionally with the addition of a brookite phase-directing mineralizer (e.g., AlCl 3 ⁇ 6H 2 O, ⁇ -Al 2 O 3 , and Al(OH) 3 ).
  • a brookite phase-directing mineralizer e.g., AlCl 3 ⁇ 6H 2 O, ⁇ -Al 2 O 3 , and Al(OH) 3 ).
  • Amorphous hydrous titanium oxide precipitate (sometimes represented as TiO(OH) 2 ⁇ nH 2 O with n ⁇ 32) is added to water to produce a slurry typically in the 33 - 50 wt % range.
  • the slurry can be acidified with strong mineral acids to give pH values typically in the 1 - 2 range.
  • metal chloride salts can be added at levels ranging from 0.5 to 20% of the weight of the amorphous TiO(OH) 2 ⁇ nH 2 O.
  • rutile TiO 2 of pigmentary size (100 nm - 300 nm) can be formed at 250 °C - 374 °C with the addition of a rutile-directing mineralizer (e.g., ZnCl 2 , ZnO, MgCl 2 , or NaCl).
  • a rutile-directing mineralizer e.g., ZnCl 2 , ZnO, MgCl 2 , or NaCl.
  • the slurry is placed into gold reaction tubes, which are then crimped closed, rather than fully sealed, to allow for pressure equilibration.
  • the gold tube with its contents is then placed into an autoclave.
  • the temperature can range from 250 °C to 374 °C and the pressure is autogenous, typically ranging from 40 to 170 atm, respectively.
  • the duration of the high temperature hydrothermal treatment is generally from 1 to 72 h.
  • Iron oxide can be produced from the iron-rich precipitates produced in the above described processes.
  • the iron-rich precipitates are reacted with a base, preferably aqueous trimethylamine, in the presence of oxygen, to form an iron oxide/hydroxide and a di-trimethylammonium oxalate solution derived from the iron-rich precipitates.
  • the iron oxides are then separated from the solution.
  • Iron oxide may be used as a pigment or in the production of metallic iron.
  • the iron(II)-rich precipitates can be oxidized by treatment in an oxalate solution to soluble iron(III) species that are subsequently hydrolyzed with aqueous trimethylamine to give an iron oxide/hydroxide precipitate and an a ditrimethylammonium oxalate solution.
  • the iron-rich precipitates can be calcined or hydrothermally treated to form various iron oxide phases. These routes are described in " Iron Oxides in the Laboratory” by U. Schwertmann and R. M. Georgia, Wiley VCH, 2nd Edition, Weinheim, 2003 .
  • Trimethylammonium hydrogen oxalate can be recovered and recycled from di-trimethylammonium oxalate produced in various steps and embodiments of the processes.
  • the recovered trimethylammonium hydrogen oxalate can be used for further ilmenite ore digestion.
  • Aqeuous di-trimethylammonium oxalate is derived from processing of both iron-rich solutions and titanium-rich solutions.
  • the aqueous di-trimethylammonium oxalate can be combined or processed independently.
  • the di-trimethylammonium oxalate solutions are heated to remove trimethylamine with water from aqueous trimethylammmonium hydrogen oxalate.
  • the ability to recycle the oxalate-containing reagents and aqueous trimethylamine reduces the operating cost of the process.

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Claims (5)

  1. Procédé comprenant:
    a) la digestion de minerai ilménite avec de l'hydrogéno oxalate de triméthylammonium aqueux pour former un lixiviat et un précipité riche en fer;
    b) la séparation dudit lixiviat dudit précipité riche en fer;
    c) l'hydrolyse dudit lixiviat avec de la triméthylamine ou de la triméthylamine aqueuse pour former de l'hydroxyde de titanyle et une solution riche en oxalate;
    d) la séparation dudit hydroxyde de titanyle de ladite solution riche en oxalate;
    e) le lavage dudit hydroxyde de titanyle avec un matériau sélectionné dans le groupe constitué de l'eau, de la triméthylamine et de la triméthylamine aqueuse pour former de l'hydroxyde de titanyle à faible teneur en oxalate; et
    f) la cristallisation du dioxyde de titane dudit hydroxyde de titanyle à faible teneur en oxalate.
  2. Procédé selon la revendication 1 comprenant en outre l'addition d'un agent réducteur audit lixiviat pour former un lixiviat réduit et un second précipité riche en fer et la séparation dudit second précipité riche en fer dudit lixiviat réduit.
  3. Procédé selon la revendication 1 comprenant en outre:
    l'oxydation dudit précipité riche en fer dans une solution acide d'hydrogéno oxalate de triméthylammonium pour former une solution d'oxalate de triméthylammonium fer (III);
    optionnellement, la séparation du minerai n'ayant pas réagi de ladite solution de triméthylammonium fer (III)
    l'addition d'une base à ladite solution d'oxalate de triméthylammonium fer (III) pour former un précipité d'hydroxyde riche en fer et une solution d'oxalate de ditriméthylammonium;
    la séparation dudit précipité d'hydroxyde riche en fer de ladite solution d'oxalate de di-triméthylammonium; et
    optionnellement, la calcination dudit précipité d'hydroxyde riche en fer.
  4. Procédé selon la revendication 1, comprenant en outre:
    l'addition d'une base audit précipité riche en fer pour former un précipité d'hydroxyde riche en fer et une solution basique;
    la séparation dudit précipité d'hydroxyde riche en fer de ladite solution basique; et
    optionnellement, la calcination dudit précipité d'hydroxyde riche en fer.
  5. Procédé selon la revendication 1, comprenant en outre la calcination dudit précipité riche en fer.
EP08797260.0A 2008-08-06 2008-08-06 Procédés de fabrication de dioxyde de titane Active EP2310322B1 (fr)

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KR (1) KR20110043735A (fr)
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CN102112399B (zh) 2015-03-25
JP2011530469A (ja) 2011-12-22
KR20110043735A (ko) 2011-04-27
MX2011001286A (es) 2011-03-21
EP2310322A1 (fr) 2011-04-20
AU2008360391A1 (en) 2010-02-11
CN102112399A (zh) 2011-06-29
WO2010016835A1 (fr) 2010-02-11

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